Hydrogen generation systems

ABSTRACT

A system for production of hydrogen includes a steam methane reformer (SMR) including an outer tube, wherein a first end of the outer tube is closed; and an inner tube disposed in the outer tube, wherein a first end of the inner tube is open. An SMR flow channel is defined within the inner tube and an annular space is defined between the outer tube and the inner tube. The flow channel is in fluid communication with the annular space. The SMR includes a foam disposed in the annular space. The system includes a water gas shift reactor comprising a reaction tube, wherein a reaction channel is defined within the reaction tube, and wherein the reaction channel is in fluid communication with the SMR flow channel; a heat transfer material disposed in the reaction channel; and a catalyst disposed in the reaction channel.

CROSS-REFERENCE TO RELATED APPLICATION

This application is a continuation of U.S. patent application Ser. No.16/821,605, now U.S. Pat. No. 10,894,244, filed Mar. 17, 2020, which isincorporated herein by reference in its entirety.

BACKGROUND

Hydrogen generation reactions convert hydrocarbons, such as methane,into hydrogen gas. Hydrogen gas can be used, e.g., as fuel for vehicles.

SUMMARY

We describe here systems for energy-efficient, low-emission productionof hydrogen gas (H2) from hydrocarbons. The systems include a steammethane reactor (SMR) having a bayonet flow path in which incomingreactant fluid flowing along the flow path is heated by transfer ofrecovered heat from outgoing fluid flowing along the flow path.Catalytic foam and heat transfer foam disposed along the bayonet flowpath catalyze a hydrogen generation reaction in the SMR and facilitateheat transfer to the incoming reactant fluid. Product fluid from the SMRis provided to a water gas shift (WGS) reactor. The fluid flows acrossone or more WGS catalysts and one or more heat transfer materialsdisposed along a reaction channel in the WGS reactor. The WGS catalystsand heat transfer material catalyze a hydrogen generation reaction inthe WGS and facilitate removal of heat generated by the exothermic WGShydrogen generation reaction. Cooling fluid heated by heat from the WGShydrogen generation reaction can be provided as input into the SMR. Theuse of heat transfer among fluid streams in the SMR enables energyefficient production of hydrogen to be achieved.

In a general aspect, a system for production of hydrogen includes asteam methane reformer (SMR) including an outer tube, wherein a firstend of the outer tube is closed; and an inner tube disposed in the outertube, wherein a first end of the inner tube is open. An SMR flow channelis defined within the inner tube and an annular space is defined betweenthe outer tube and the inner tube. The flow channel is in fluidcommunication with the annular space. The SMR includes a foam disposedin the annular space between the outer tube and the inner tube. Thesystem includes a water gas shift (WGS) reactor including a reactiontube, wherein a WGS reaction channel is defined within the reactiontube, and wherein the WGS reaction channel is in fluid communicationwith the SMR flow channel; a heat transfer material disposed in the WGSreaction channel; and a WGS catalyst disposed in the WGS reactionchannel.

Embodiments can include one or any combination of two or more of thefollowing features.

An outlet of the SMR flow channel is in fluid communication with aninlet of the WGS reaction channel.

The WGS reactor includes a housing, the reaction tube of the WGS reactorbeing disposed in the housing, and wherein a cooling fluid channel isdefined between the housing and the reaction tube of the WGS reactor. Anoutlet of the cooling fluid channel is in fluid communication with aninlet of the annular space of the SMR. An inlet of the WGS reactionchannel and an outlet of the cooling fluid channel are disposed at afirst end of the WGS reactor. The WGS reactor includes a flow controllerconfigured to control a flow rate of cooling fluid through the coolingfluid channel.

The foam of the SMR includes an SMR catalyst. The SMR catalyst isdisposed on the foam of the SMR. The SMR catalyst is configured tocatalyze an SMR hydrogen generation reaction in which hydrogen andcarbon monoxide are produced. The SMR includes an outer heat exchangefoam disposed in the annular space between the outer tube and the innertube, wherein a distance between the outer heat exchange foam and asecond end of the outer tube is less than a distance between the foamassembly and the second end of the outer tube.

The SMR includes an inner heat exchange foam disposed in the SMR flowchannel.

A bayonet flow path through the SMR is defined from an inlet at a secondend of the outer tube, along the annular space between the outer tubeand the inner tube toward the first end of the outer tube, along the SMRflow channel, and to an outlet at a second end of the inner tube.

The WGS catalyst includes a foam including a WGS catalyst material. TheWGS catalyst material includes a foam substrate, wherein the WGScatalyst material is disposed on the foam substrate.

The WGS catalyst includes: a first WGS catalyst disposed in the WGSreaction channel and configured to catalyze a hydrogen generationreaction in a first temperature range; and a second WGS catalystdisposed in the WGS reaction channel and configured to catalyze thehydrogen generation reaction in a second temperature range lower thanthe first temperature range. The heat transfer material is disposed inthe WGS reaction channel between the first WGS catalyst and the secondWGS catalyst.

The heat transfer material disposed in the WGS reaction channel includesa foam.

The system includes a furnace, wherein a portion of the SMR is disposedin the furnace. The first end of the outer tube of the SMR is disposedin the furnace. The system includes an external heat transfer materialdisposed on an outer surface of the outer tube of the SMR.

In a general aspect, combinable with the previous aspect, a method forproducing hydrogen includes flowing a first gas along a bayonet flowpath of a steam methane reformer (SMR) to produce a first product,including flowing the first gas through a foam disposed along thebayonet flow path; providing the first product produced in the SMR to aninput of a water gas shift (WGS) reaction channel defined within areaction tube of a WGS reactor; and flowing a second gas including thefirst product through the WGS reaction channel to produce a secondproduct. Flowing the second gas includes flowing the second gas across aheat transfer material disposed in the WGS reaction channel to reducethe temperature of the flowing second gas; and flowing the second gasacross a WGS catalyst disposed in the reaction channel.

Embodiments can include one or any combination of two or more of thefollowing features.

Flowing the first gas along the bayonet flow path of the SMR includesflowing the first gas from an annular space into an SMR flow channel,wherein the annular space is defined between an outer tube and an innertube disposed within the outer tube and the SMR flow channel is definedwithin the inner tube. Flowing the first gas along the bayonet flow pathof the SMR includes flowing the first gas from an inlet at a second endof the outer tube, along the annular space toward a first end of theouter tube, along the SMR flow channel defined within the inner tube,and to an outlet at a second end of the inner tube. The method includesheating the first gas flowing along the annular space with heat from thegas flowing along the flow channel defined within the inner tube.

Flowing the first gas through a foam disposed along the bayonet flowpath includes flowing the gas through a catalytic foam.

The method includes flowing a cooling fluid through a cooling fluid flowpathway defined between a housing of the WGS reactor and the reactiontube of the WGS reactor. Contacting the flowing second gas to the heattransfer material disposed in the WGS reaction channel includestransferring heat from the flowing second gas to the cooling fluid. Themethod includes heating the cooling fluid to a temperature of between100° C. and 300° C. The method includes providing heated cooling fluidfrom the cooling fluid flow pathway to an input of the bayonet flow pathof the SMR. The method includes providing heated cooling fluid from thecooling fluid flow pathway to an input of the WGS reaction channel. Themethod includes adjusting a flow rate of the cooling fluid through thecooling fluid flow pathway based on a rate at which the first product isprovided to the input of the WGS reaction channel.

The method includes providing the first product to the input of the WGSreaction channel at a temperature equal to or greater than a temperatureat which the WGS catalyst structure catalyzes a hydrogen generationreaction. The method includes providing the first product to the inputof the WGS reaction channel at a temperature of between 200° C. and 450°C.

Flowing the second gas across the WGS catalyst includes: flowing thesecond gas across a first WGS catalyst disposed in the WGS reactionchannel, wherein the first WGS catalyst is configured to catalyze ahydrogen generation reaction in a first temperature range; and flowingthe second gas across a second WGS catalyst disposed in the reactionchannel, wherein the second WGS catalyst is configured to catalyze thehydrogen generation reaction in a second temperature range lower thanthe first temperature range. The method includes flowing the second gasacross the heat transfer material after flowing the second gas acrossthe first WGS catalyst.

Flowing the second gas to the heat transfer material includes reducingthe temperature of the flowing second gas to a temperature at which theWGS catalyst is capable of catalyzing a hydrogen generation reaction.

The method includes flowing the first gas along the bayonet flow path ofthe SMR to produce carbon monoxide and hydrogen. Providing the firstproduct to the input of the WGS reaction channel includes providingcarbon monoxide to the input of the WGS reaction channel.

The method includes flowing the second gas along the WGS reactionchannel to produce carbon dioxide and hydrogen.

In a general aspect, combinable with any of the previous aspects, asteam methane reformer (SMR) system includes an outer tube, wherein afirst end of the outer tube is closed; an inner tube disposed in theouter tube, wherein a first end of the inner tube is open. A flowchannel is defined within the inner tube and an annular space is definedbetween the outer tube and the inner tube, the flow channel being influid communication with the annular space. The SMR system includes acatalytic foam disposed in the annular space between the outer tube andthe inner tube, the catalytic foam including a catalyst.

Embodiments can include one or any combination of two or more of thefollowing features.

The catalytic foam includes a foam substrate, wherein the catalyst isdisposed on the foam substrate.

The SMR system includes an outer heat exchange foam disposed in theannular space between the outer tube and the inner tube. A distancebetween the outer heat exchange foam and a second end of the outer tubeis less than a distance between the catalytic foam and the second end ofthe outer tube. The e outer heat exchange foam has an annular shape.

The catalytic foam has an annular shape.

The SMR system includes an inner heat exchange foam disposed in the flowchannel.

The catalytic foam contacts the inner tube.

A thickness of the catalytic foam is equal to a width of the annularspace.

The catalytic foam has a porosity of between 10 pores per inch (ppi) and30 ppi.

A length of the catalytic foam along the inner tube is between 10 inchesand 5 feet.

A length of the catalytic foam in an externally heated section of theouter tube is between 10% and 30% of a length of the outer tube.

The catalytic foam includes a metal foam. The catalytic foam includesnickel.

The catalytic foam includes silicon carbide.

A bayonet flow path through the SMR system is defined from an inlet at asecond end of the outer tube, along the annular space between the outertube and the inner tube toward the first end of the outer tube, alongthe flow channel, and to an outlet at a second end of the inner tube.

A ratio between a cross-sectional area of the flow channel and across-sectional area of the annular space is between 1 and 5.

The inner tube is coaxial with the outer tube.

A width of the annular space between the outer tube and the inner tubeis between 0.2 inches and 4 inches.

A length of the outer tube is between 8 feet and 30 feet.

The SMR system includes an elongated baffle disposed in the flowchannel.

The SMR system includes a heat transfer material disposed on an outersurface of the first end of the outer tube. The heat transfer materialincludes a fin disposed on the outer surface of the first end of theouter tube. The heat transfer material includes a baffle disposed on theouter surface of the first end of the outer tube. The heat transfermaterial includes a foam disposed on the outer surface of the first endof the outer tube.

In a general aspect, combinable with any of the previous aspects, amethod for producing hydrogen in a steam methane reformer (SMR) systemincludes flowing a gas along a bayonet flow path of the SMR system. Thebayonet flow path is defined by an annular space defined between anouter tube and an inner tube disposed in the outer tube, wherein a firstend of the outer tube is closed and a first end of the inner tube isopen; a flow channel defined within the inner tube, wherein the flowchannel is in fluid communication with the annular space. Flowing thegas along the bayonet flow path includes flowing the gas through acatalytic foam disposed in the annular space between the outer tube andthe inner tube.

Embodiments can include one or any combination of two or more of thefollowing features.

Flowing the gas along the bayonet flow path includes flowing the gasthrough an outer heat exchange foam disposed in the annular spacebetween the outer tube and the inner tube.

The method includes flowing the gas through the outer heat exchange foambefore flowing the gas through the catalytic foam.

Flowing the gas along the bayonet flow path includes flowing the gasthrough an inner heat exchange foam disposed in the flow channel.

Flowing the gas along the bayonet flow path includes flowing the gasfrom the annular space into the flow channel. The method includesflowing the gas from the annular space at the first end of the outertube into the flow channel at the first end of the inner tube.

The method includes heating the gas flowing in the annular space withheat from the gas flowing in the flow channel defined within the innertube.

The method includes heating the gas in the annular space at the firstend of the outer tube.

The method includes flowing the gas along at least a portion of thebayonet flow path in turbulent flow.

The method includes producing hydrogen from the gas flowing along thebayonet flow path.

In an aspect, combinable with any of the previous aspects, a water gasshift (WGS) reactor system includes a housing; a reaction tube disposedin the housing, wherein a reaction channel is defined within thereaction tube and a cooling fluid channel is defined between the housingand the reaction tube; a catalyst disposed in the reaction channel, thecatalyst configured to catalyze a hydrogen generation reaction; and aheat transfer material disposed in the reaction channel.

Embodiments can include one or any combination of two or more of thefollowing features.

The catalyst includes a first catalyst disposed in the reaction channeland configured to catalyze the hydrogen generation reaction in a firsttemperature range; and a second catalyst disposed in the reactionchannel and configured to catalyze the hydrogen generation reaction in asecond temperature range lower than the first temperature range. Theheat transfer material is disposed in the reaction channel between thefirst catalyst and the second catalyst. The first catalyst is configuredto catalyze the hydrogen generation reaction at a temperature of between200° C. and 450° C. The second catalyst is configured to catalyze thehydrogen generation reaction at a temperature of between 180° C. and350° C.

A distance between the heat transfer material and an inlet of thereaction channel is less than a distance between the catalyst structureand the inlet of the reaction channel. The catalyst includes a catalystconfigured to catalyze the hydrogen generation reaction at a temperatureof between 200° C. and 450° C.

The catalyst includes a foam including a catalyst material. Thecatalytic foam includes a foam substrate, wherein the catalyst materialis disposed on the foam substrate. The foam has a porosity of between 5pores per inch (ppi) and 30 ppi.

The catalyst includes catalyst pellets.

The heat transfer material includes a foam. The foam has a porosity ofbetween 5 ppi and 30 ppi.

The heat transfer material includes a fin.

The WGS reactor system includes a cooling channel heat transfer materialdisposed in the cooling fluid channel. The cooling channel heat transfermaterial includes a foam.

The housing includes a cylindrical housing, and wherein the reactiontube is coaxial with the cylindrical housing.

The WGS reactor system includes an inner tube disposed in the reactiontube, wherein the reaction channel is defined by an annular spacebetween the reaction tube and the inner tube, and wherein an innercooling fluid channel is defined within the inner tube.

The WGS reactor system includes multiple reaction tubes disposed in thehousing.

An inlet of the reaction channel and an outlet of the cooling fluidchannel are disposed at a first end of the WGS reactor.

An inlet of the reaction channel is in fluid communication with anoutlet of the cooling fluid channel.

An outlet of the cooling fluid channel is configured to be in fluidcommunication with an inlet of a steam methane reformer (SMR).

The WGS reactor system includes a flow controller configured to controla flow rate of cooling fluid through the cooling fluid channel.

In a general aspect, a method for producing hydrogen in a water gasshift (WGS) reactor includes flowing a cooling fluid through a coolingfluid channel defined between a housing of a WGS reactor and a reactiontube disposed in the housing; and flowing a gas including carbonmonoxide and steam through a reaction channel defined within thereaction tube. Flowing the gas through the reaction channel includesflowing the gas across a heat transfer material disposed in the reactionchannel to transfer heat from the flowing gas to the cooling fluid inthe cooling fluid channel; and flowing the gas across a catalystdisposed in the reaction channel, the catalyst configured to catalyze ahydrogen generation reaction.

Embodiments can include one or any combination of two or more of thefollowing features.

Flowing the gas across the heat transfer material includes reducing thetemperature of the flowing gas to a temperature at which the catalyststructure catalyzes the hydrogen generation reaction. The methodincludes reducing the temperature of the flowing gas to between 200° C.and 450° C.

Flowing the gas across the catalyst includes flowing the gas across afirst catalyst disposed in the reaction channel, wherein the firstcatalyst is configured to catalyze the hydrogen generation reaction in afirst temperature range; and flowing the gas across a second catalystdisposed in the reaction channel, wherein the second catalyst isconfigured to catalyze the hydrogen generation reaction in a secondtemperature range lower than the first temperature range. The methodincludes receiving the gas into the reaction channel at a temperaturewithin the first temperature range. The method includes receiving thegas into the reaction channel at a temperature of between 200° C. and450° C. The method includes flowing the gas across the heat transfermaterial after flowing the gas across the first catalyst. Flowing thegas across the heat transfer material includes reducing the temperatureof the flowing gas to within the second temperature range. The methodincludes reducing the temperature of the flowing gas to between 180° C.and 350° C.

The method includes flowing cooling fluid through an inner cooling fluidchannel defined within an inner tube disposed in the reaction tube.

Flowing the gas through the reaction channel includes flowing the gasfrom a first end of the WGS reactor to a second end of the WGS reactor;and wherein flowing the cooling fluid through the cooling fluid channelincludes flowing the cooling fluid from the second end of the WGSreactor to the first end of the WGS reactor.

The method includes adjusting a flow rate of the cooling fluid throughthe cooling fluid channel based on a flow rate of the gas through thereaction channel.

The method includes outputting the cooling fluid from the cooling fluidchannel at a temperature of between 100° C. and 300° C.

The method includes providing steam from the cooling fluid channel to aninput of the reaction channel.

The method includes providing steam from the cooling fluid channel to aninput of a steam methane reformer.

The approaches described here can have one or more of the followingadvantages. The use of recuperated heat to heat and cool fluid streamsto target temperatures enables the hydrogen generation process to be anenergy efficient, low-emission process. The systems can be modular,e.g., enabling a target throughput to be achieved by change in systemconfiguration or operation. The systems can be scalable for large-scale,energy efficient hydrogen generation.

The details of one or more implementations are set forth in theaccompanying drawings and the description below. Other features andadvantages will be apparent from the description and drawings, and fromthe claims.

BRIEF DESCRIPTION OF DRAWINGS

FIG. 1 is a diagram of a hydrogen generation system.

FIG. 2A is a cross sectional view of a steam methane reformer (SMR).

FIG. 2B is a cross-sectional view of the SMR of FIG. 2A along the lineA-A′.

FIG. 2C is a cross-sectional view of the SMR of FIG. 2A along the lineB-B′.

FIG. 3 is a diagram of a water gas shift (WGS) reactor.

FIG. 4 is a diagram of a WGS reactor.

FIG. 5 is a diagram of a WGS reactor.

FIG. 6 is a diagram of a hydrogen generation system.

FIG. 7 is a process flow chart.

FIG. 8 is a plot of the temperature differential between the inner andouter tubes of an SMR.

FIGS. 9A and 9B are simulations of heat transfer in an SMR with andwithout a foam, respectively.

DETAILED DESCRIPTION

We describe here systems for energy-efficient, low-emission productionof hydrogen gas (H2) from hydrocarbons. The systems include a steammethane reactor (SMR) having a bayonet flow path in which incomingreactant fluid flowing along the flow path is heated by transfer ofrecovered heat from outgoing fluid flowing along the flow path.Catalytic foam and heat transfer foam disposed along the bayonet flowpath catalyze a hydrogen generation reaction in the SMR and facilitateheat transfer to the incoming reactant fluid. Product fluid from the SMRis provided to a water gas shift (WGS) reactor. The fluid flows acrossone or more WGS catalysts and one or more heat transfer materialsdisposed along a reaction channel in the WGS reactor. The WGS catalystsand heat transfer material catalyze a hydrogen generation reaction inthe WGS and facilitate removal of heat generated by the exothermic WGShydrogen generation reaction. Cooling fluid heated by heat from the WGShydrogen generation reaction can be provided as input into the SMR. Theuse of heat transfer among fluid streams in the SMR enables energyefficient production of hydrogen to be achieved.

The hydrogen generation systems described here are modular and have asmall footprint. The systems can be upgraded or turned down withoutsignificant downtime. Elements of the systems, such as tubes, manifolds,flanges, and catalysts, can be taken apart or replaced easily, enablingmaintenance or operational adjustments with low downtime.

Referring to FIG. 1 , a schematic diagram of a hydrogen generationsystem 100, shown in an operational configuration, includes a steammethane reactor (SMR) 200 and a water gas shift (WGS) reactor 300 thattogether generate hydrogen gas (H2) from hydrocarbons, such as naturalgas, biogas, methane, methanol, or other suitable hydrocarbons. Fluid102, including hydrocarbons and water vapor (steam) is input into theSMR and reacted in the presence of a catalytic foam. Recuperated heatfrom fluid flowing through the SMR 200 and externally applied heat raisethe temperature of the reactants flowing through the SMR 200 to atemperature at which the SMR hydrogen generation reaction occurs.Heating of the reactants using residual heat from fluid flowing throughthe SMR reduces the heating load on an external heat source, therebyenabling energy efficient operation. Product gas 104 generated in theSMR includes hydrogen gas and carbon monoxide.

At least a portion of the product gas 104 (e.g., hydrogen and carbonmonoxide), along with steam, is provided as fluid input into the WGSreactor 300. For energy efficient operation, the product gas 104 isoutput from the SMR at a temperature appropriate for input into the WGSreactor 300, thereby enabling active heating or cooling of the fluidinput into the WGS reactor 300 to be avoided. The fluid input into theWGS reactor 300 flows along a reaction channel of the WGS reactor 300and reacts in the presence of a WGS catalyst, such as a catalytic foam,to produce hydrogen and carbon dioxide. A heat exchange material, suchas a foam, is disposed in the reaction channel and transfers excess heatgenerated by the exothermic WGS hydrogen generation reaction to acooling fluid 108 flowing through the WGS reactor 300. Cooling of thefluid in the reaction channel by heat transfer facilitated by the heatexchange material allows active cooling in the WGS reactor 300 to beavoided, enabling energy efficient operation. Product gas 110 generatedin the WGS includes hydrogen gas and carbon dioxide. Heated coolingfluid 106, in the form of steam, can be provided as part of the fluid102 input into the SMR 200. In some examples, additional steam isprovided from an external water source, e.g., for system startup.

Referring to FIGS. 2A-2C, the SMR 200 includes two concentric tubes, anouter tube 202 and an inner tube 204 disposed coaxially in the outertube 202. A first end of the outer tube 202 at a first end 206 of theSMR 200 is closed and a first end of the inner tube 204 is open. Anannular space 210 is defined between the outer tube 202 and the innertube 204. A flow channel 212 is defined within the inner tube 204 and isin fluid communication with the annular space 210. An elongated baffle213 is disposed along at least a portion of the length of the inner tube204.

Fluid (e.g., gas) flowing through the SMR 200 follows a bayonet flowpath (indicated by arrows in FIG. 2A) through the SMR 200 from an inlet214 into the annular space 210 at a second end 216 of the SMR 200, alongthe annular space 210 toward the first end of the outer tube 202 at thefirst end 206 of the SMR, into the flow channel 212, along the flowchannel 212 toward a second end of the inner tube 204 at the second end216 of the SMR, and to an outlet 220 at the second end of the inner tube204. Reactants (e.g., hydrocarbons and water) are input into the bayonetflow path at the inlet 214. A hydrogen generation reaction occurs towardthe first end 206 of the outer tube in the presence of an SMR catalyst,generating products (e.g., hydrogen gas and carbon monoxide) that areoutput from the SMR 200 via the outlet 220. An example hydrogengeneration reaction that occurs in the SMR 200 is represented asfollows:CH₄+H₂O→3H₂+CO.

The hydrogen generation reaction is an endothermic reaction that occursabove a reaction temperature, such as between 600° C. and 1000° C. Anexternal heat source 222 heats the fluid flowing along the annular space210 at the first end 206 of the SMR 200 to at least the reactiontemperature. The external heat source 222 can be driven by combustion(e.g., a gas-powered furnace), solar energy, or another appropriateenergy source.

Fluid in the annular space 210 at the first end 206 of the SMR 200 isheated by the external heat source 222. The heated fluid flows from theannular space 210 at the first end 206 of the SMR 200 into the flowchannel 212, entering the flow channel at high temperature. The bayonetflow path of the SMR, in which the outer and inner tubes 202, 204 (andhence the annular space 210 and flow channel 212) are concentric,provides a configuration in which heat from the high-temperature fluidflowing along the flow channel 212 can be transferred back to thelower-temperature fluid flowing along the annular space 210. The innertube 204 is designed to facilitate this heat transfer, e.g., the innertube 204 can be formed of a material with high thermal conductivity,such as a metal or silicon carbide, and can have thin walls. The use ofrecuperated heat to raise the temperature of the fluid flowing along theannular space 210 lessens the load on the external heat source 222,improving the energy efficiency of the hydrogen generation reaction. Inaddition, when the external heat source 222 is a combustion furnace, areduced load on the furnace reduces hydrocarbon consumption of theexternal heat source 222, thereby reducing emissions associated with thehydrogen generation reaction.

Referring specifically to FIGS. 2A and 2B, a catalytic foam 230 isdisposed in the annular space 210 between the outer tube 202 and theinner tube 204. The catalytic foam 230 includes an SMR catalyst thatcatalyzes the hydrogen generation reaction (e.g., the generation ofhydrogen and carbon monoxide from hydrocarbons and water). The hydrogengeneration reaction occurs primarily in the portions of the bayonet flowpath in which the catalytic foam 230 is disposed, and that are at atemperature at or above the reaction temperature. For instance, thehydrogen generation reaction occurs in portions of the bayonet flow paththat are heated by the external heat source 222, such as in a heatedportion 221 of the annular space 210 toward the first end 206 of the SMR200 and in an end space 223 at the first end 206 of the SMR 200. Thehydrogen generation reaction can also occur in regions outside theheated portion 221, e.g., regions that are heated to or above thereaction temperature by heat transfer from fluid flowing along the flowchannel 212 (discussed further below).

In some examples, the SMR catalyst is coated onto a foam substrate toform the catalytic foam 230. In some examples, the SMR catalyst isintegrated or impregnated into a foam substrate to form the catalyticfoam 230. The catalytic foam 230 is a porous structure through which oneor more fluid flow paths are defined from an upstream side 232 to adownstream side 234 of the catalytic foam 230. As fluid flows along thebayonet flow path through the SMR 200, the fluid flows through the fluidflow paths of the catalytic foam 230 and the catalyst in the catalyticfoam 230 catalyzes the hydrogen generation reaction in the flowingfluid. The porosity of the catalytic foam 230 provides a high surfacearea for contact between the catalytic foam 230 and the flowing fluid,which facilitates efficient catalysis of the hydrogen generationreaction.

The catalytic foam 230 includes a thermally conductive material suchthat the catalytic foam 230 also facilitates heat transfer to the fluidflowing through the catalytic foam 230 from the external heat source222, the fluid flowing along the flow channel 212 in the inner tube 202,or both. Physical contact between the catalytic foam 230 and the outertube 202 enables transfer of heat from the external heat source 222 tothe fluid flowing through the catalytic foam. Physical contact betweenthe catalytic foam 230 and the inner tube 204 enables transfer of heatfrom the fluid flowing along the flow channel 212 to the fluid flowingthrough the catalytic foam. The high surface area of the catalytic foam230 facilitates heat transfer. The porosity of the catalytic foam 230also can lead to turbulent fluid flow in at least a portion of theannular space 210, further facilitating heat transfer to the fluidflowing along the annular space 210 and enhancing the energy efficiencyof the hydrogen generation process.

The catalytic foam 230 has an annular shape. As shown in FIGS. 2A and2B, a thickness t_(c) of the annulus of the catalytic foam 230 (referredto simply as the thickness of the catalytic foam 230) is equal to theradial distance between the outer wall of the inner tube 204 and theinner wall of the outer tube 202 (referred to as the width of theannular space 210) such that the catalytic foam 230 is in physicalcontact with both the outer tube 202 and the inner tube 204. Contactbetween the catalytic foam 230 and the outer and inner tubes 202, 204enables heat transfer from the external heat source 222 and the fluidflowing along the flow channel 212 in the inner tube 202 to the fluidflowing through the catalytic foam 230. In some examples, the thicknesst_(c) of the catalytic foam 230 is less than the width of the annularspace 210 and the catalytic foam 230 is in physical contact with onlyone of the tubes, such as with only the outer tube 204 or only the innertube 204.

The porosity of the catalytic foam 230 (e.g., pores per inch) and lengthof the catalytic foam 230 (referring to the length of the catalytic foamalong the axis of the outer tube 202 from the upstream side 232 to thedownstream side 234 of the catalytic foam 230) affect the surface areaof the catalytic foam 230, thus affecting the efficiency of catalysisand heat transfer. Increased porosity and length both increase theopportunity for contact between the flowing fluid and the catalytic foam230, thereby enhancing the efficiency of both catalysis and heattransfer. The length of the catalytic foam 230 also affect the drop influid pressure that occurs across the catalytic foam 230 as fluid flowsthrough the catalytic foam 230. Increased porosity and length both causeincreased pressure drop across the catalytic foam 230, which can slowfluid flow along the bayonet flow path, reducing throughput of the SMR200. The porosity and length of the catalytic foam 230 can be selectedto achieve efficient catalysis and heat transfer with low pressure dropacross the catalytic foam 230. For instance, the catalytic foam 230 canhave a porosity of between 10 pores per inch (ppi) and 30 ppi. In someexamples, the catalytic foam 230 is entirely within the heated portion221 of the outer tube 202 (as in the example of FIG. 2A), e.g., thelength l_(c) of the catalytic foam 230 is between 10% and 30% of thelength of the heated portion 221 of the outer tube 202, such as between10 inches and 5 feet in length. In some examples, the catalytic foam 230extends beyond the heated portion 221 of the outer tube 202 and canextend up to the entire length of the outer tube. In some examples, theporosity and length of the catalytic foam 230 can be selected such thata fluid pressure drop of less than 1 pound per square inch (psi) occursacross the catalytic foam 230.

The catalytic foam 230 includes a material (e.g., the foam substrate)having a thermal conductivity sufficient to facilitate heat transfer tofluid flowing through the catalytic foam 230, e.g., heat transfer fromthe fluid flowing along the flow channel 212, heat transfer from theexternal heat source 222, or both. The material of the catalytic foam230 is non-reactive to the fluid (e.g., the reactants and products ofthe hydrogen generation reaction) flowing along the bayonet flow path ofthe SMR 200 in the temperature range at which the SMR 200 is operated.The material of the catalytic foam 230 can be thermally compatible with,e.g., have a similar thermal expansion coefficient as, the material ofthe outer tube 202, the inner tube 204, or both, e.g., to avoiddelamination of the catalytic foam 230 from the tubes 202, 204. Forinstance, the foam can be a metal foam, such as a nickel or stainlesssteel foam, or a silicon carbide foam; or another suitable material.

Referring to FIG. 2A, an outer heat exchange foam 250 formed of athermally conductive material is disposed in the annular space 210between the outer tube 202 and the inner tube 204. A distance betweenthe outer heat exchange foam 250 and the inlet 214 at the second end 216of the outer tube 202 is less than a distance between the catalytic foam230 and the inlet 214, such that fluid flowing along the annular space210 flows through the outer heat exchange foam 250 prior to flowingthrough the catalytic foam 230. The outer heat exchange foam 250 is inphysical contact with the inner tube 204 and facilitates heat transferfrom the fluid flowing along the flow channel 212 to the fluid flowingthrough the outer heat exchange foam 250.

Referring also to FIG. 2C, an inner heat exchange foam 252 formed of athermally conductive material is disposed in the flow channel 212defined within the inner tube 204. The inner heat exchange foam 252 isin physical contact with the inner tube 204 and facilitates heattransfer from fluid flowing through the inner heat exchange foam 252 tothe fluid flowing along the annular space 210. The porosity of the outerand inner heat exchange foams 250, 252 provide a high surface area forcontact between the foams 250, 252 and the fluid flowing through therespective foam, which facilitates efficient heat transfer. The porosityof the outer and inner heat exchange foams 250, 252 also can lead toturbulent fluid flow in at least a portion of the annular space 210 orthe flow channel 212, respectively, further facilitating heat transfer.In some examples, a catalytic foam can be disposed in the flow channel212, e.g., in addition to or instead of the inner heat exchange foam252.

The heat transfer enabled by the outer and inner heat exchange foams250, 252 enables the fluid in the annular space 210 to be preheatedbefore the fluid reaches the catalytic foam 230, using excess heatrecovered from the higher temperature fluid flowing along the flowchannel 212. The use of recuperated heat to preheat the fluid flowingalong the annular space 210 can reduce the amount of heat provided bythe external heat source 222 to heat the fluid flowing along the annularspace 210 to the reaction temperature, thereby enhancing the efficiencyof the SMR 200.

The outer heat exchange foam 250 has an annular shape. A thickness ofthe annulus of the outer heat exchange foam 250 (referred to as thethickness of the outer heat exchange foam 250) is equal to the width ofthe annular space 210 such that the outer heat exchange foam 250 is inphysical contact with both the outer tube 202 and the inner tube 204. Insome examples, the thickness of the outer heat exchange foam 250 is lessthan the width of the annular space 210 and the outer heat exchange foam250 is in physical contact with only one of the tubes, such as with onlythe inner tube 204.

The inner heat exchange foam 252 also has an annular shape. A thicknesst_(i) of the annulus of the inner heat exchange foam 252 is equal to theradial distance between the inner tube 204 and the elongated baffle 213such that the inner heat exchange foam 252 is in physical contact withthe inner tube 204. In some examples, the thickness t_(i) of the innerheat exchange foam 252 is less than the radial distance and the innerheat exchange foam 252 is in physical contact with the inner tube 204but not with the elongated baffle 213. In some examples, the elongatedbaffle 213 is not present, and the inner heat exchange foam 252 isannular or cylindrical, with a thickness that is equal to or less thanthe radius of the flow channel 212.

The porosity and length of each of the outer heat exchange foam 250 andthe inner heat exchange foam 252 can be selected to achieve efficientheat transfer with low pressure drop across the respective heat exchangefoam 250, 252. For instance, each of the heat exchange foams 250, 252can have a porosity of between 10 pores per inch (ppi) and 30 ppi. Thelength of the outer heat exchange foam 250 can be as small as, e.g., 4inches, and as long as the distance between the inlet 212 and theupstream side 232 of the catalytic foam 230. The length of the innerheat exchange foam 252 can be as small as, e.g., 4 inches, and as longas the distance between the first end 208 of the inner tube 204 and theoutlet 220 at the second end 218 of the inner tube 204. In someexamples, the porosity and length of the outer and inner heat exchangefoams 250, 252 can be selected such that a pressure drop of less than 1pound per square inch (psi) occurs across the each of the outer andinner heat exchange foams 250, 252. In some examples, the outer heatexchange foam 250, the inner heat exchange foam 252, or both are notpresent.

The outer and inner heat exchange foams 250, 252 are formed of amaterial having a thermal conductivity sufficient to facilitate heattransfer to the fluid flowing along the annular space 210. The materialof the heat exchange foams 250, 252 is non-reactive to the fluid (e.g.,the reactants and products of the hydrogen generation reaction) flowingalong the bayonet flow path of the SMR 200 in the temperature range atwhich the SMR 200 is to be operated. The material of the outer and innerheat exchange foams 250, 252 can be thermally compatible with, e.g.,have a similar thermal expansion coefficient as the inner tube 204,e.g., to avoid delamination. For instance, the heat exchange foams 250,252 can be metal foams, such as nickel or stainless steel foams; orsilicon carbide foams; or another suitable material.

The presence of the catalytic foam 230 and the outer and inner heatexchange foams 250, 252 along the bayonet flow path enables both highthroughput through the SMR 200 and energy efficient operation of the SMR200. For instance, heating the fluid flowing along the annular space 210with recuperated heat from the higher temperature fluid flowing alongthe flow channel 212 enables the reaction temperature to be reached withless input of heat from the external heat source 222, providing forenergy efficient SMR operation. In addition, by heating the fluidflowing along the annular space 210 with recuperated heat, the annularspace 210 can be made relatively wide, such as between 0.2 inches and 4inches, which can accommodate relatively high volume gas flow.

Referring to FIG. 2A, a heat transfer material 258 is disposed on anouter surface of the first end 206 of the outer tube 202 to facilitateheat transfer from the external heat source 222 to the fluid flowingalong the bayonet flow path of the SMR 200. In the example of FIG. 2A,the heat transfer material 258 is a fin; in some examples, the heattransfer material 258 can be a baffle, a foam, or another structuresuitable for facilitating heat transfer. The heat transfer material 258enhances the efficiency of heat transfer from the external heat source222 to the fluid flowing along the annular space 210, contributing tothe energy efficient operation of the SMR by increasing the amount ofheat produced by the external heat source 222 that is used to heat thefluid in the bayonet flow path.

The locations, lengths, and properties (e.g., porosity, thermalconductivity) of the catalytic foam 230 and the inner and outer heatexchange foams 250, 252 can be selected to achieve a desired temperatureat one or more points along the bayonet flow path. For instance, thefoam locations, lengths, and properties can be selected to achieve atarget temperature at the catalytic foam 230 to facilitate a highefficiency hydrogen generation reaction. In some examples, fluid outputfrom the SMR is provided to a WGS reactor to act as a reactant in afurther hydrogen generation reaction, and the foam locations and lengthscan be selected to achieve a target temperature of fluid output from theoutlet 220 of the flow channel 212, such as a target temperature forinput into the WGS reactor. By outputting fluid from the SMR 200 at thetarget temperature for input into the WGS reactor, the use of externalheat sources for preheating WGS reactor inputs can be reduced oreliminated, enhancing the overall efficiency of the system.

The catalytic foam 230 and outer and inner heat transfer foams 250, 252can be removed from the SMR 200 and replaced, e.g., with foams ofdifferent characteristics (e.g., different porosity, length, thermalconductivity, or other characteristics). For instance, exchanging one ormore of the foams can help a desired performance to be achieved, such asa target throughput or a target temperature of the output fluid from theSMR 200.

In some examples, the length of the outer tube 202 is between 8 feet and30 feet, e.g., for a modular hydrogen generation system. In someexamples, the outer tube 202 can be longer, e.g., for an industrialplant scale hydrogen generation system. The width of the annular spacecan be between 0.2 inches and 4 inches. The ratio between across-sectional area of the flow channel 212 and a cross-sectional areaof the annular space 210 (see FIG. 2B) is greater than one, e.g.,between 1 and 5, to accommodate the increase in moles of gas resultingfrom the hydrogen generation reaction.

In some examples, the catalytic foam 230, outer heat transfer foam 250,inner heat transfer foam 252, or a combination of any two or more ofthem is a non-uniform structure, e.g., having a non-uniform porosity ora multimaterial composition. For instance, in locations at which fluidpressure drop across a foam is less important, the foam can beconfigured with smaller pores to enhance heat transfer. The foam can bea multimaterial foam, e.g., a foam having an outer shell of nickel forchemical compatibility with an inner shell of aluminum or copper forheat transfer efficiency. In some examples, the outer heat transfer foam250, the inner heat transfer foam 252, or both can be replaced by asolid, cylindrical tube.

Heat transfer in the SMR (e.g., heat transfer from fluid flowing alongthe flow channel to fluid flowing along the annular space 210) isrelated to the pressure of the flowing fluid. Increased fluid pressuregenerally results in increased heat transfer. The walls of the inner andouter tubes 202, 204 for an SMR operating at high pressure are thickerthan the walls of the inner and outer tubes 202, 204 for an SMRoperating at lower pressure. The increased wall thickness can reduceheat transfer. SMR components (e.g., wall thickness for the inner andouter tubes) and operating parameters (e.g., fluid pressure) can bedesigned to balance such competing factors.

In the example of FIGS. 2A-2C, the SMR 200 includes a single set oftubes that includes the outer tube 202 and the inner tube 204. In someexamples, an SMR includes multiple sets of tubes, each set having anouter tube and an inner tube. The multiple sets of tubes can be operatedin parallel for increased throughput and can be heated by a singleexternal heat source 222 sized to generate sufficient heat for themultiple sets of tubes.

The products of the hydrogen generation reaction in the SMR 200,including hydrogen gas and carbon monoxide, along with excess steam, areoutput from the SMR 200 via the outlet 220. The SMR output is providedas input to a water gas shift (WGS) reactor, where carbon monoxide andwater (e.g., steam) are reacted in the presence of a WGS catalyst togenerate hydrogen gas and carbon dioxide.

The output from the SMR 200 is at a temperature sufficient for inputinto the WGS reactor. The WGS reactor includes one or more WGScatalysts, each of which operates in a respective temperature range, andthe SMR output is at a temperature at or above the temperature range ofthe WGS catalyst such that external, active heating of the SMR outputdoes not occur prior to input into the WGS reactor. The temperature ofthe SMR output is controllable by adjustment of parameters that affectheat transfer between the fluid flowing along the flow channel 212 andthe fluid flowing along the annular space 210 of the SMR, e.g.,characteristics of the outer heat transfer foam 250, the inner heattransfer foam 252, diameters and materials of the outer and inner tubes202, 204, flow rate of fluid along the bayonet flow path, or otherfactors.

Referring to FIG. 3 , an example WGS reactor 300 includes a housing 302and a reaction tube 304 disposed in the housing 302. A reaction channel306 is defined within the reaction tube 304. For instance, the housing302 and the reaction tube 304 both can be cylindrical tubes, with thereaction tube 304 coaxial with the cylindrical housing 302. In theexample of FIG. 3 , the reaction channel 306 is an annular space definedbetween the reaction tube 304 and an inner tube 308 disposed in thereaction tube 304. In some examples, the reaction channel 306 iscylindrical and no inner tube is disposed in the reaction tube 304.

Reactant fluid, such as the fluid output from the SMR, enters into aninlet 305 of the reaction channel 306 at a first end 310 of the WGSreactor 300 and flows along the reaction channel 306. A hydrogengeneration reaction occurs along the reaction channel 306 in thepresence of a WGS catalyst that is disposed in the reaction channel 306.The hydrogen generation reaction generates products (e.g., hydrogen gasand carbon dioxide) that are output from the reaction channel 306 via anoutlet 307 at a second end 312 of the WGS reactor. For instance, theinlet 305 of the reaction channel 306 at the first end 310 of the WGSreactor 300 is in fluid communication with the outlet 220 of the SMR 200(see FIG. 2A), and fluid output from the SMR is provided into thereaction channel 306 of the WGS 300. An example of the WGS hydrogengeneration reaction is represented as follows:CO+H₂O→H₂+CO₂.

The hydrogen generation reaction in the WGS 300 is an exothermicreaction. Heat generated by the hydrogen generation reaction in the WGS300 is removed by cooling fluid, such as water, flowing along a coolingfluid channel 314 defined between the housing 302 of the WGS and thereaction tube 304. Cooling fluid can also flow through an inner coolingfluid channel 316 defined within the inner tube 308. The cooling fluidenters into an inlet of each the cooling fluid channel 314 and the innercooling fluid channel 316 at the second end 312 of the WGS reactor 300,and exits from an outlet of each the cooling fluid channel 314 and theinner cooling fluid channel 316 at the first end 310 of the WGS reactor.The direction of flow of the fluid in the reaction channel 308 is fromthe first end 310 to the second end 312 of the WGS reactor 300; thedirection of flow of the cooling flow is the opposite, from the secondend 312 to the first end 310 of the WGS reactor 300. As the coolingfluid flows along the cooling fluid channel 314 and the inner coolingfluid channel 316, the cooling fluid is heated with heat from the fluidflowing along the reaction channel 308. In some examples, the coolingfluid is liquid water at the inlets and is heated such that the coolingfluid is steam, or a mixture of liquid water and steam, at the outlets.

A WGS catalyst and a heat transfer material are disposed in the reactionchannel 306 of the WGS reactor 300. The configuration of the WGScatalyst and the heat transfer material can be adjusted, e.g., toachieve a target throughput or hydrogen generation efficiency, toachieve operation in a target temperature range, or to achieve anothergoal. For instance, the position of the WGS catalyst and the heattransfer material along the reaction channel 306 can be adjusted. Thestructure and extent of the WGS catalyst and the heat transfer materialcan be adjusted. In the example of FIG. 3 , the WGS reactor 300 isconfigured as a two-catalyst system with a heat transfer material 334disposed between two WGS catalysts 330, 332. In the example of FIG. 4 ,the WGS reactor 300 is configured as a one-catalyst system, with a heattransfer material 434 and a single WGS catalyst 430. Otherconfigurations of WGS catalysts and heat transfer materials are alsopossible.

In the two-catalyst configuration of the WGS reactor 300 shown in FIG. 3, a first WGS catalyst 330 and a second WGS catalyst 332 are disposed inthe reaction channel 306. The first WGS catalyst 330 catalyzes the WGShydrogen generation reaction in a first temperature range, e.g., between200° C. and 450° C. The first WGS catalyst 330 can be a high temperatureWGS catalyst that catalyzes the WGS hydrogen generation reaction attemperatures of, e.g., between 310° C. and 450° C. The first WGScatalyst 330 can be a medium temperature WGS catalyst that catalyzes theWGS hydrogen generation reaction at temperatures of, e.g., between 200°C. and 350° C. The reactants are input into the reaction channel 306 ata temperature within the first temperature range such that the first WGScatalyst 330 can catalyze the hydrogen generation reaction in the gasflowing across the first WGS catalyst 330.

The second WGS catalyst 332 is disposed further along the reactionchannel 306 such that the distance between the first WGS catalyst 330and the inlet 305 of the reaction channel 306 is less than the distancebetween the second WGS catalyst 332 and the inlet 305 of the reactionchannel 306. Gas flowing along the reaction channel 306 flows across thefirst WGS catalyst 330 before flowing across the second WGS catalyst332. The second WGS catalyst 332 catalyzes the WGS hydrogen generationreaction in a second temperature range that is lower than the firsttemperature range. For instance, the second WGS catalyst 332 catalyzesthe WGS hydrogen generation reaction in a temperature range of, e.g.,between 180° C. and 350° C. When the first WGS catalyst 330 is a hightemperature WGS catalyst, the second WGS catalyst 332 can be a mediumtemperature WGS catalyst; or the second WGS catalyst 332 can be a lowtemperature WGS catalyst that catalyzes the WGS hydrogen generationreaction at temperatures of, e.g., between 180° C. and 250° C. When thefirst WGS catalyst 330 is a medium temperature WGS catalyst, the secondcatalyst 332 can be a low temperature WGS catalyst.

A heat transfer material 334 is disposed in the reaction channel 306between the first WGS catalyst 330 and the second WGS catalyst 332, withthe distance between the heat transfer material 334 and the inlet 305 ofthe reaction channel 306 being less than the distance between the secondWGS catalyst 332 and the inlet 305 of the reaction channel 306. Fluidflowing along the reaction channel 306 first flows across the first WGScatalyst 330, then across the heat transfer material 334, and thenacross the second WGS catalyst 332. The heat transfer material 334 is inphysical contact with the reaction tube 304, the inner tube 308, orboth. The heat transfer material 334 facilitates in-situ transfer ofheat from the fluid flowing along the reaction channel 306 (e.g., heatgenerated by the exothermic hydrogen generation reaction that occurs atthe first catalyst 330) to the cooling fluid flowing along the coolingfluid channel 314, the inner cooling fluid channel 316, or both. Thisheat transfer reduces the temperature of the gas flowing along thereaction channel to the temperature range at which the second WGScatalyst 332 can catalyze the hydrogen generation reaction.

In some examples, an input side heat transfer material (not shown) isdisposed in the reaction channel 306 such that fluid received into thereaction channel 306 flows across the input side heat transfer materialprior to flowing across the first catalyst 330. This input side heattransfer material reduces the temperature of the fluid to thetemperature range at which the first WGS catalyst 330 can catalyze thehydrogen generation reaction. For instance, when fluid from the SMR 200(FIG. 2 ) is provided as input into the WGS 300 at a temperature that istoo high for the first WGS catalyst 330, the input side heat transfermaterial reduces the temperature of the input fluid to the temperaturerange of the first WGS catalyst 330. In some examples, an output sideheat transfer material (not shown) is disposed in the reaction channel306 such that fluid flows across the output side heat transfer materialafter flowing across the second catalyst 332. This output side heattransfer material facilitates recovery of heat into the cooling fluidafter completion of the WGS hydrogen generation reaction, enhancing theenergy efficiency of the WGS reactor.

Heat transfer materials 336, 338 are disposed in the cooling fluidchannel 314 and in the inner cooling fluid channel 316, respectively.Cooling fluid flowing along the cooling fluid channel 314 and the innercooling fluid channel 316 flows across the heat transfer materials 336,338, respectively. The heat transfer material 336 is in physical contactwith the reaction tube 304 to facilitate transfer of heat from the fluidflowing along the reaction channel 306 to the cooling fluid flowingalong the cooling fluid channel 314. The heat transfer material 338 isin physical contact with the inner tube 308 to facilitate transfer ofheat from the fluid flowing along the reaction channel 306 to thecooling fluid flowing along the inner cooling fluid channel 316.

As the cooling flow flows along the cooling fluid channels 314, 316, thecooling fluid is heated by heat transfer from the fluid flowing alongthe reaction channel. In some examples, the heated cooling fluid isprovided as input to the SMR 200 or returned as input to the reactionchannel 306 of the WGS 300. For instance, the heated cooling fluid canbe saturated water or two-phase water (liquid/steam) produced at atemperature and flow rate appropriate for input into the SMR.

In the configuration of the WGS reactor 300 shown in FIG. 3 , the heattransfer materials 336, 338 are aligned with the heat transfer material334. In some examples, the heat transfer materials 336, 338 are notaligned with the heat transfer material 334. The heat transfer materials336, 338 can extend along some or all of the length of the cooling fluidchannel 314 and inner cooling fluid channel 316, respectively. In someexamples, only one of the heat transfer materials 336, 338 is present,or neither of the heat transfer materials 336, 338 is present.

The catalyst arrangement in the WGS reactor 300 enables activation andreduction of a single catalyst without affecting the other catalyst. Ingeneral, the catalyst(s) in the WGS reactor 300 are activated by slowlyflowing a reducing gas across the catalyst at a slightly elevatedtemperature to reduce the catalyst to a metallic, active form. In someexamples, the WGS catalyst(s) are activated externally prior toconnection of the WGS to the SMR.

Referring to FIG. 4 , the WGS reactor 300 is configured as asingle-catalyst system in which a single WGS catalyst 430 is disposed inthe reaction channel 306 of the WGS reactor 300. The WGS catalyst 430catalyzes the WGS hydrogen generation reaction at temperatures of, e.g.,between 200° C. and 450° C. The WGS catalyst 430 can be a hightemperature WGS catalyst or a medium temperature WGS catalyst.

A heat transfer material 434 is disposed in the reaction channel 306such that a distance between the heat transfer material 434 and theinlet 305 of the reaction channel 306 is less than the distance betweenthe WGS catalyst 430 and the inlet 305 of the reaction channel 306.Fluid flowing along the reaction channel 306 first flows across the heattransfer material 434 and then flows across the WGS catalyst 430. Theheat transfer material 434 is in physical contact with the reaction tube304, the inner tube 308, or both, and facilitates the transfer of heatfrom the fluid received into the reaction channel 306 to the coolingfluid flowing along the cooling fluid channel 314, the inner coolingfluid channel 316, or both. This heat transfer reduces the temperatureof the fluid to within a temperature range at which the WGS catalyst 430can catalyze the WGS hydrogen generation reaction. For instance, whencarbon monoxide output from the SMR 200 (FIG. 2 ) is provided as inputinto the WGS 300 at a temperature that is too high for the WGS catalyst430, the heat transfer material 434 reduces the temperature of the inputfluid to the temperature range of the catalyst 430.

Heat transfer materials 436, 438 are disposed in the cooling fluidchannel 314 and in the inner cooling fluid channel 316, respectively,and facilitate heat transfer from the fluid flowing along the reactionchannel 306 to the cooling fluid flowing along the cooling fluid channel314 and the inner cooling fluid channel 316. In the configuration of theWGS reactor 300 shown in FIG. 4 , the heat transfer materials 436, 438are aligned with the heat transfer material 434. In some examples, theheat transfer materials 436, 438 are not aligned with the heat transfermaterial 434. The heat transfer materials 436, 438 can extend along someor all of the length of the cooling fluid channel 314 and inner coolingfluid channel 316, respectively. In some examples, only one of the heattransfer materials 436, 438 is present, or neither of the heat transfermaterials 436, 438 is present.

The WGS catalysts 330, 332, 430 of FIGS. 3 and 4 can be pellets, beads,saddles, rings, or other structures formed of a catalyst material. TheWGS catalysts 330, 332, 430 can be catalytic foams, foils, fins, orother structures that include a substrate and a catalyst material, e.g.,with the catalyst material disposed on or integrated into the substrate.A catalytic foam is a porous structure through which one or more flowpaths are defined. The porosity of the catalytic foam can be selected toachieve a high surface area, enabling efficient catalysis, as well as alow pressure drop across the catalytic foam, enabling efficient fluidflow along the reaction channel 306. For instance, the catalytic foamcan have a porosity of between 5 ppi and 30 ppi. The material of thecatalytic foam is non-reactive to the fluid (e.g., the reactants andproducts of the WGS hydrogen generation reaction) flowing along thereaction channel 306 in the temperature range at which the WGS 300 isoperated. For instance, the catalytic foam can be a metal foam, such ascopper or aluminum, or a silicon carbide film, or another suitablematerial. In the two-catalyst configuration of FIG. 3 , the first andsecond WGS catalysts 330, 332 both can have the same structure, or eachof the first and second WGS catalysts 330, 332 can have a distinctstructure.

The heat transfer materials 334, 336, 338, 434 are materials having athermal conductivity sufficient to enable heat transfer from the fluidflowing along the reaction channel 306 to the cooling fluid flowingalong the cooling fluid channel 314 or the inner cooling fluid channel316 or both. The heat transfer materials 334, 434 disposed in thereaction channel 306 are non-reactive to the fluid (e.g., the reactantsand products of the WGS hydrogen generation reaction) flowing along thereaction channel 306 in the temperature range at which the WGS 300 isoperated. For instance, the heat transfer materials 334, 434 can be ametal, such as copper or aluminum, or silicon carbide, or anothersuitable material.

The heat transfer materials 334, 336, 338, 434 can be foams, fins,foils, rings, saddles, beads, or pellets, or other structures capable ofheat transfer. In the example of a foam, the porosity and length of thefoam can be selected to achieve a high surface area, enabling efficientheat transfer, as well as a low pressure drop across the foam, enablingefficient fluid flow along the reaction channel 306. For instance, theheat transfer materials 334, 336, 338, 434 can be foams having aporosity of between 5 ppi and 30 ppi.

Referring to FIGS. 3 and 4 , the flow rate of cooling fluid along thecooling fluid channels 314, 316 is controlled by a flow controller 340.The flow rate can be selected or adjusted based on the temperature ofthe fluid input into the reaction channel 306, the temperature of thecooling fluid input into the cooling fluid channels 314, 316. The flowrate can be selected or adjusted based on a target output temperature ofthe fluid output from the reaction channel 306, a target outputtemperature of the cooling fluid, or both. The flow rate can be selectedor adjusted based on the catalyst configuration, the type of catalyst(s)(e.g., high-, medium-, or low-temperature WGS catalyst), or both. Theflow rate can be selected or adjusted based on an actual or desiredthroughput.

Cooling of the fluid in the reaction channel 306 of the WGS reactor 300enables the WGS hydrogen generation reaction to be carried out at highenergy efficiency. The transfer of heat from the fluid in the reactionchannel 306 to the cooling fluid cools the fluid in the reaction channel306, e.g., removing heat generated during the exothermic hydrogengeneration reaction and reducing the temperature of the fluid to anappropriate temperature range for the WGS catalyst(s), with noenergy-intensive active cooling of the fluid. Moreover, the heattransfer in the WGS reactor enables isothermal conditions to beachieved, improving the conversion efficiency of the WGS hydrogengeneration reaction.

Referring to FIG. 5 , a WGS reactor 500 includes multiple reaction tubes504 a-504 c disposed in a housing 502. A reaction channel 506 a-506 c isdefined within each reaction tube 504 a-504 c (collectively referred toas reaction tubes 504). Reactant gas flows into the reaction channels506 a-506 c (collectively referred to as reaction channels 506) at afirst end 510 of the WGS reactor 500, and product gas exits the reactionchannels 506 at a second end 512 of the WGS reactor 500.

A cooling fluid channel 514 is defined in the space between the housing502 and the reaction tubes 504. Cooling fluid enters into the coolingfluid channel 514 at the second end 512 of the WGS reactor and exitsfrom the cooling fluid channel at the first end 510 of the WGS reactor500.

In the example of FIG. 5 , the WGS reactor 500 is a single-catalystsystem, with a single catalyst 522, such a high temperature WGS catalystor a medium temperature WGS catalyst, disposed in each reaction channel506. A heat transfer material 524 is disposed in each reaction channels506 to facilitate heat transfer from the gas in the reaction channel 508to the cooling fluid in the cooling fluid channel 514. In some examples,the WGS reactor 500 including multiple reaction tubes can be configuredas a two-catalyst system.

Referring to FIG. 6 , the SMR 200 and WGS 300 are integrated into asystem 600 for production of hydrogen gas (H2) from hydrocarbons. Acombustion furnace 602 as the external heat source heating the first endof the SMR 200. The system 600 also can be implemented with the WGS 500,with an SMR including multiple sets of outer and inner tubes, or both.

The hydrogen generation reaction in the SMR 200 produces hydrogen gas(H2) and carbon monoxide (CO) from reactants including hydrocarbons andwater vapor (steam) in the presence of a catalytic foam including an SMRcatalyst. The hydrogen gas and carbon monoxide are output from the flowchannel defined within the inner tube of the SMR onto an SMR productline 604 along with excess steam. The fluid (e.g., hydrogen gas, carbonmonoxide, and steam) from the SMR 200 are provided as input to thereaction channel of the WGS 300. The outlet of the SMR 200 is in fluidcommunication with the inlet of the WGS 300 via the SMR product line604. In some examples, additional steam is provided into the reactionchannel of the WGS 300, e.g., from a water storage 614 (discussed infra)or from a cooling fluid output line 620 from the WGS 300 (discussedinfra) to achieve a target ratio of steam to carbon monoxide.

As discussed supra, the fluid flowing along the flow channel toward theoutlet of the SMR 200 is cooled by heat transfer with the incoming fluidflowing along the annular space of the SMR. The temperature of the fluidat the outlet of the SMR is thus at least partially controllable by theextent of heat transfer with the fluid in the annular space. The heattransfer, and thus the outlet fluid temperature, is affected by theconfiguration of the SMR 200 (e.g., the position, length, porosity, orother characteristics of the catalytic foam and the heat exchange foams)and by the operation of the SMR (e.g., the flow rate of fluid along thebayonet flow path of the SMR 200). The configuration, operation, or bothof the SMR 200 can be adjusted to achieve heat transfer such that thefluid output from the SMR 200 is at a temperature appropriate for inputinto the reaction channel of the WGS 300. For instance, when the WGS 300is configured with a high- or medium-temperature WGS catalyst toward theinput of the reaction channel, the SMR 200 can be configured such thatthe carbon monoxide and steam arrive at the reaction channel of the WSG300 with a temperature in the range at which the WGS catalyst is active.By making use of heat transfer within the SMR 200 to achieve a targettemperature for fluid output from the SMR, external, active coolingdevices are not used between the SMR 200 and the WGS 300, and the roleof external, active heating devices (e.g., the furnace 602) can bereduced, thus contributing to high energy efficiency of the system-levelhydrogen generation process.

The hydrogen generation reaction in the WGS 300 produces hydrogen gasand carbon dioxide (CO2), which are output from the reaction channel ofthe WGS 300 onto a WGS product line 608 along with excess steam. Theexcess steam is removed from the fluid on the WGS product line 608 in avapor liquid separator (VLS) 610. The remaining hydrogen gas and carbondioxide are sent downstream 611 for separation, with the carbon dioxidediscarded (e.g., via a flue stack, discussed infra) and the hydrogen gasremoved to a hydrogen storage, e.g., for use as fuel. The separatedsteam flows along a steam line 612 to a water storage 614, which alsostores water provided from an external water source 616. The separatedsteam on the steam line 612, the water from the external water source616, or both can be treated before storage in the water storage 614.

Water from the water storage 614 is provided along a cooling fluid line618 as cooling fluid input into the WGS 300. The heated cooling fluidoutput from the WGS 300, which is a mixture of liquid water and steam,flows along a cooling fluid output line 620. The heated cooling fluidwill ultimately be provided as an input reactant into the SMR 200. Thetemperature of the heated cooling fluid output from the WGS 300 isaffected by the configuration of the WGS 300 (e.g., the type, position,or other characteristics of the WGS catalyst and the heat transfermaterial(s)) and by the operation of the WGS 300 (e.g., the flow rate offluid along the reaction channel and the flow rate of cooling fluid).The configuration, operation, or both of the WGS 300 can be adjustedsuch that the heated cooling fluid is output at a target temperature,such as a temperature sufficient for input into the SMR 200. By heatingthe cooling fluid to a target temperature using recovered heat from thefluid in the WGS 300 reaction channel, external, active heating elementsto heat the SMR input fluid are not used. In addition, external, activecooling are not used to remove heat from the exothermic WGS hydrogengeneration reaction. The use of recovered heat to heat the SMR inputfluid and the cooling of the exothermic WGS hydrogen generation reactioncontributes to high system-level energy efficiency.

The heated cooling fluid output from the WGS 300 flows along the coolingfluid output line 620 to an accumulator 622. The accumulator 622 alsoreceives additional water from the water storage 614 along a water line624. Steam and water output from the accumulator 622 onto an accumulatoroutput line 626 is heated in a heat exchanger 634 with heat from fluegases 636 from the combustion furnace 602. Hydrocarbons provided via ahydrocarbon line 630 are heated in a heat exchanger 635 with heat fromthe flue gases 636. The heated steam and hydrocarbons 632, 633,respectively, are mixed in a mixer 628 and output onto an SMR input line638, which feeds the heated steam and hydrocarbons to the inlet of theouter tube of the SMR 200. The use of recovered heat from the flue gases636 to heat the mixture of steam and hydrocarbons to a temperaturesufficient for input into the SMR contributes to high system-levelenergy efficiency. In this configuration, the outlet of the WGS coolingfluid flow channels is in fluid communication with the inlet of the SMR200 such that the heated WGS cooling fluid ultimately is provided as acomponent of the fluid input into the SMR 200. The flue gases 636, afterpassing through the heat exchanger 634, are discarded to a flue gasstack 640.

Referring to FIG. 7 , in operation of a hydrogen generation systemincluding an SMR and a WGS reactor, a fluid (e.g., a gas) includingreactants is provided as input (700) to an SMR. Specifically, the fluidis provided into an inlet of an annular space of the SMR at a second endof the SMR, with the annular space being defined between an outer tubeand an inner tube of the SMR. The fluid provided to the inlet includeshydrocarbons, e.g., methane, natural gas, biogas, methanol, or otherhydrocarbons. The fluid provided to the inlet also includes steam.

The fluid flows along a bayonet flow path of the SMR. Specifically, thefluid flows (702) along the annular space from the second end to thefirst end of the SMR. Along the annular space, the fluid flows throughan outer heat exchange foam (704) that facilitates heat transfer fromhigh-temperature fluid flowing along a flow channel defined in the innertube of the SMR to the lower-temperature fluid flowing along the annularspace. The outer heat exchange foam also can induce turbulent flow inthe fluid flowing along the annular space, enhancing the heat transferefficiency.

The fluid flowing along the annular space is heated (706) by an externalheat source, such as a combustion furnace, toward the first end of theSMR. In the heated region of the SMR, the fluid flows through acatalytic foam (708), which catalyzes the SMR hydrogen generation toproduce hydrogen gas and carbon monoxide from the hydrocarbon and steamreactants (710). The catalytic foam facilitates heat transfer to the gasflowing therethrough, e.g., heat transfer from higher-temperatureproduct fluid flowing along the flow channel within the inner tube ofthe SMR and heat transfer from the external heat source.

The fluid, now at higher temperature and including hydrogen and carbonmonoxide, flows (712) from the annular space into the flow channel atthe first end of the SMR. The fluid in the flow channel flows from thefirst end of the SMR toward the second end of the SMR, opposite thedirection of flow of fluid in the annular space. The fluid in the flowchannel flows through an inner heat exchange foam (714) that facilitatesheat transfer from high-temperature fluid flowing along the flow channelto the lower-temperature fluid flowing along the annular space. Theinner heat exchange foam also can induce turbulent flow in the fluidflowing along the flow channel, enhancing the heat transfer efficiency.The presence of an elongated baffle in the inner tube also enhances heattransfer efficiency.

When the fluid flowing along the flow channel reaches the SMR outlet,the fluid (including hydrogen gas, carbon monoxide, and steam) is outputfrom the SMR (716) at the second end of the SMR. The SMR output fluid isprovided as input into a reaction channel of a WGS reactor (720). Theheat transfer between fluid flowing along the annular space and fluidflowing along the flow channel in the SMR can result in the carbonmonoxide being at a temperature sufficient for input into the WGSreactor, such as a temperature in or above a temperature range at whicha WGS catalyst can catalyze the WGS hydrogen generation reaction. Forinstance, the fluid output from the SMR and provided as input into thereaction channel of the WGS reactor is at a temperature of between 200°C. and at least 450° C.

Fluid including carbon monoxide and steam flow along the reactionchannel of the WGS reactor (722), flowing across one or more WGScatalysts and one or more heat transfer materials. Cooling fluid, suchas water, flows along one or more cooling fluid channels (724). Thedirection of fluid flow along the reaction channel is opposite thedirection of fluid flow along the cooling fluid channels. The flow rateof the cooling fluid can be adjusted (726), e.g., based on a flow rateof the fluid flow along the reaction channel (e.g., which is based onthroughput of the SMR), based on a target output temperature for thecooling fluid, or based on a configuration or operation of the WGS.

In the example of FIG. 7 , the WGS reactor is configured as atwo-catalyst system, e.g., as shown in FIG. 3 . The fluid in thereaction channel flows across a first WGS catalyst (728), e.g., ahigh-temperature or medium-temperature WGS catalyst. The first WGScatalyst catalyzes the WGS hydrogen generation reaction in a firsttemperature range (730), e.g., between 200° C. and 450° C., to producehydrogen gas and carbon dioxide. The fluid in the reaction channel thenflows across a heat transfer material disposed in the reaction channel(732). The heat transfer material reduces the temperature of the fluidto a second temperature range in which a second WGS catalyst operates byheat transfer to the cooling fluid flowing in the cooling fluidchannel(s). The heat transfer raises the temperature of the coolingfluid, e.g., to between 100° C. and 300° C. The fluid in the reactionchannel, now in the second temperature range, flows across a second WGScatalyst (734), e.g., a medium-temperature or low-temperature WGScatalyst. The second WGS catalyst catalyzes the WGS hydrogen generationreaction in a second temperature range (736) lower than the firsttemperature range, e.g., between 180° C. and 250° C. to produce hydrogengas and carbon dioxide.

Fluid, including hydrogen gas, carbon dioxide, and excess steam, isoutput from the reaction channel of the WGS reactor (738). The excesssteam is separated (740) and the separated steam, along with coolingfluid (e.g., a mixture of steam and liquid water) from the WGS reactor,are recycled (742) to be used, e.g., as input into the WGS reactionchannel or as input into the SMR.

EXAMPLES

Simulations and experiments of heat transfer in an SMR were performed toevaluate the role of catalytic foam in transferring heat from theexternal heat source to the fluid flowing along the annular space of theSMR.

Referring to FIG. 8 , foams of differing porosities were disposed in theannular space of an SMR. For each foam type, the SMR was heated to 400°C. and the temperature differential between the outer tube and the innertube was measured by thermocouple. The temperature differential for eachof three foams (10 ppi, 20 ppi, and 30 ppi), and the temperaturedifferential for an empty annular space (no foam) is shown in FIG. 8 . Alower temperature differential indicates temperature equilibration dueto heat transfer. The measured temperature differential between outerand inner tubes was about 50° C. greater when no foam was used than whena foam was present, indicating lack of heat conduction without foam andeffective heat conduction with foam.

Referring to FIGS. 9A and 9B, the heat transfer characteristics of anSMR 150 were simulated to demonstrate the effect of foam on heattransfer from an external heat source into the SMR. The SMR 150 has anouter tube 152 and an inner tube 154, with an annular space 160 definedbetween the outer tube 152 and the inner tube 154, and a flow channel162 defined within the inner tube 152. FIGS. 9A and 9B show a crosssection of only half of the SMR; the axis X-X′ is the axis along thecenter of the flow channel 162. An external heat source 172 suppliesheat to a heated portion 171 of the SMR. In FIG. 9A, a foam 180 isdisposed in the annular space 160. In FIG. 9B, no foam is present in theannular space (FIG. 9B). Other parameters, including inlet fluid flowrate, inlet fluid temperature, annular width, and tube dimensions, werethe same. The heat source 172 was simulated as a section of the outertube 152 maintained at 875° C. As can be seen from FIGS. 9A and 9B, withthe foam 180 present in the annular space 130 (FIG. 9A), the fluid inthe annular space 160 reached a temperature of over 760° C., while inthe SMR without foam (FIG. 9B), the fluid in the annular space 160reached a temperature of only 450° C. The foam 180 present in theannular space also resulted in increased temperature of the fluid in theflow channel 162 within the inner tube 152, e.g., by heat transfer andby flow of heated fluid from the annular space 160 into the flow channel162. These results demonstrate the effective heat transfer provided byfoam disposed in the annular space of an SMR.

Particular embodiments of the subject matter have been described. Otherembodiments are within the scope of the following claims.

What is claimed is:
 1. A system for production of hydrogen, the systemcomprising: a steam methane reformer (SMR) comprising: an outer tube,wherein a first end of the outer tube is closed; an inner tube disposedin the outer tube, wherein a first end of the inner tube is open,wherein an SMR flow channel is defined within the inner tube and anannular space is defined between the outer tube and the inner tube, theSMR flow channel being in fluid communication with the annular space; anSMR foam disposed in at least a portion of the annular space between theouter tube and the inner tube; and a water gas shift (WGS) reactorcomprising: a housing; and a reaction tube disposed in the housing,wherein the WGS reaction channel is defined within the reaction tube,and wherein the WGS reaction channel is in fluid communication with theSMR flow channel, and wherein the WGS reactor comprises a WGS catalystdisposed in the WGS reaction channel.
 2. The system of claim 1 whereinan outlet of the SMR flow channel is in fluid communication with aninlet of the WGS reaction channel.
 3. The system of claim 1, wherein acooling fluid channel is defined between the housing and the reactiontube of the WGS reactor.
 4. The system of claim 1, wherein an outlet ofthe cooling fluid channel is in fluid communication with an inlet of theannular space of the SMR.
 5. The system of claim 1, wherein an inlet ofthe WGS reaction channel and an outlet of the cooling fluid channel aredisposed at a first end of the WGS reactor.
 6. The system of claim 1,wherein the WGS reactor comprises a flow controller configured tocontrol a flow rate of cooling fluid through the cooling fluid channel.7. The system of claim 1, wherein the SMR foam comprises an SMRcatalyst.
 8. The system of claim 7, wherein the SMR catalyst is disposedon the SMR foam.
 9. The system of claim 1, wherein the SMR comprises aninner heat exchange foam disposed in the SMR flow channel.
 10. Thesystem of claim 1, wherein a bayonet flow path through the SMR isdefined from an inlet at a second end of the outer tube, along theannular space between the outer tube and the inner tube toward the firstend of the outer tube, along the SMR flow channel, and to an outlet at asecond end of the inner tube.
 11. The system of claim 1, wherein the WGScatalyst comprises: a first WGS catalyst disposed in the WGS reactionchannel and configured to catalyze a hydrogen generation reaction in afirst temperature range; and a second WGS catalyst disposed in the WGSreaction channel and configured to catalyze the hydrogen generationreaction in a second temperature range lower than the first temperaturerange.
 12. The system of claim 11, wherein the WGS reactor comprises aheat transfer material disposed in the WGS reaction channel between thefirst WGS catalyst and the second WGS catalyst.
 13. The system of claim1, wherein the WGS reactor comprises a heat transfer material disposedin the WGS reaction channel.
 14. The system of claim 13, wherein theheat transfer material comprises a foam.
 15. The system of claim 13,wherein the SMR foam comprises an SMR catalyst.
 16. The system of claim15, wherein the SMR catalyst is disposed on the SMR foam.
 17. The systemof claim 1, comprising a furnace, wherein a portion of the SMR isdisposed in the furnace.
 18. The system of claim 17, comprising anexternal heat transfer material disposed on an outer surface of theouter tube of the SMR.
 19. A system for production of hydrogen, thesystem comprising: a steam methane reformer (SMR) comprising: an outertube, wherein a first end of the outer tube is closed; an inner tubedisposed in the outer tube, wherein a first end of the inner tube isopen, wherein an SMR flow channel is defined within the inner tube andan annular space is defined between the outer tube and the inner tube,the SMR flow channel being in fluid communication with the annularspace; an SMR foam disposed in at least a portion of the annular spacebetween the outer tube and the inner tube; and a water gas shift (WGS)reactor, wherein a WGS reaction channel is defined through the WGSreactor, and wherein the WGS reaction channel is in fluid communicationwith the SMR flow channel, and wherein the WGS reactor comprises a WGScatalyst disposed in the WGS reaction channel, and wherein the SMRcomprises an outer heat exchange foam disposed in the annular spacebetween the outer tube and the inner tube, wherein a distance betweenthe outer heat exchange foam and a second end of the outer tube is lessthan a distance between the SMR foam and the second end of the outertube.
 20. The system of claim 19, wherein the SMR foam comprises an SMRcatalyst.
 21. The system of claim 20, wherein the SMR catalyst isdisposed on the SMR foam.
 22. The system of claim 19, wherein the WGScatalyst comprises a foam comprising a WGS catalyst material.
 23. Thesystem of claim 22, wherein the WGS catalyst material comprises a foamsubstrate, wherein the WGS catalyst material is disposed on the foamsubstrate.
 24. The system of claim 19, comprising a furnace, wherein aportion of the SMR is disposed in the furnace.
 25. The system of claim24, comprising an external heat transfer material disposed on an outersurface of the outer tube of the SMR.
 26. A system for production ofhydrogen, the system comprising: a steam methane reformer (SMR)comprising: an outer tube, wherein a first end of the outer tube isclosed; an inner tube disposed in the outer tube, wherein a first end ofthe inner tube is open, wherein an SMR flow channel is defined withinthe inner tube and an annular space is defined between the outer tubeand the inner tube, the SMR flow channel being in fluid communicationwith the annular space; an SMR foam disposed in at least a portion ofthe annular space between the outer tube and the inner tube; and a watergas shift (WGS) reactor, wherein a WGS reaction channel is definedthrough the WGS reactor, and wherein the WGS reaction channel is influid communication with the SMR flow channel, and wherein the WGSreactor comprises a WGS catalyst disposed in the WGS reaction channel,and wherein the WGS catalyst comprises a foam comprising a WGS catalystmaterial.
 27. The system of claim 26, wherein the WGS catalyst materialcomprises a foam substrate, wherein the WGS catalyst material isdisposed on the foam substrate.
 28. The system of claim 26, wherein theSMR foam comprises an SMR catalyst.
 29. The system of claim 28, whereinthe SMR catalyst is disposed on the SMR foam.
 30. The system of claim26, comprising a furnace, wherein a portion of the SMR is disposed inthe furnace.
 31. The system of claim 30, comprising an external heattransfer material disposed on an outer surface of the outer tube of theSMR.